Preparation of metal hydrides



United States Patent 3,387,949 PREPARATION OF METAL HYDRIDES John C. Snyder, Darling, Pa, assignor to Hercules incorporated, a corporation of Delaware No Drawing. Filed Mar. 30, 1962, Ser. No. 183,766 4 Claims. (Cl. 23-365) ABSTRACT OF THE DISCLOSURE A process for preparing sodium or lithium aluminum hydride by the reaction of sodium, aluminum, and hydrogen in the presence of a catalyst.

This invention relates to an improved process for the preparation of alkali metal hydrides and more particularly to the preparation of the alkali metal hydrides from the metals and hydrogen.

The alkali metal hydrides and their aluminum hydride complexes are valuable reducing agents and chemical intermediates for many chemical reactions. While it is known that metal hydrides can be prepared by hydrogenation of the corresponding metal, the reaction requires high temperatures and pressures and generally results in only low or mediocre yields. Even more diffiwhy is encountered in the production of the metal aluminum hydrides. These have previously been prepared by reacting an aluminum halide with the corresponding alkali metal hydride or in a two-step process by reacting a previously formed alkali metal aluminum hydride with aluminum halide and then reacting the aluminum hydride with alkali metal hydride. However, both of these methods waste three moles of alkali metal hydride for every mole of alkali metal aluminum hydride produced. Obviously, if these metal aluminum hydrides could be produced in one step from the elements, great savings could be accomplished, but here again yields have been low.

The syntheses of the alkali metal hydrides and mixed metal hydrides from the elements involves the reaction of gaseous hydrogen with either solid or liquid metals, when producing the simple metal hydrides. The synthesis of lithium hydride is an example of the former, and of sodium hydride, an example of the latter. In the case of the mixed metal hydrides, gaseous hydrogen must be reacted with mixtures of solid metals or with mixtures of solid and liquid metals, such as in the synthesis of lithium aluminum hydride and of sodium aluminum hydride, respectively. These reactions between gases and metals, particularly to produce solids which are practically insoluble, or of very limited solubility, are mechanically difficult and slow in absolute rate. They involve diffusion of hydrogen to the active reacting center on the metal surface, subsequent reaction, and formation of a solid product, which by its very presence impedes further reaction, particularly when it is insoluble, or of very limited solubility in any medium which can be used for reaction. The overall effect is for such reactions to occur to a very limited degree, and to be impeded from further progressing by the shielding of the surface by previously formed product.

Another difficulty in these reactions between metals and hydrogen resides in the fact that adherent surface coatings of oxide, or in some cases of nitride, practically prevent initial reaction. While such layers can generally be removed or minimized by comminution, such as by milling in a so-called inert medium or atmosphere, the active metal surface frequently Welds or rewelds to other similar surfaces, unless protected by some adsorbed species. The adsorbed species may subsequently deter reaction with hydrogen.

Now in accordance with this invention it has been found that the alkali metal hydrides and mixed metal hydrides may be synthesized under milder conditions, in shorter reaction times, and in higher conversions, and frequently to give a more reactive product, when the synthesis reactions between hydrogen and the metal or metals, or between hydrogen, metal and metal hydride is carried out in the presence of a catalyst and further when the process is carried out in such a fashion that the reactants and products are continuously or intermittently subjected to comminution during the reaction. The direct synthesis of the alkali metal hydrides and mixed metal hydrides can, in accordance with this invention, be carried out more rapidly, under milder conditions, to a greater conversion or to give more reactive products, or a combination of these, if carried out in the presence of catalysts comprising transition metals or their compounds, or if such catalyst materials are mixed or alloyed with the original metal or metals. Thus, in accordance with this invention, any transition metal, metal hydride, or metal halide can be used to catalyze the synthesis of the alkali metal hydrides or mixed metal hydrides from the elements. The transition metals, or their compounds, that may be so used are the metals of Groups IVB, V-B, or VI-B of the Periodic Table, which groups include titanium, Zirconium, hafnium, vanadium, niobium, tantalum, chromium and molybdenum. The transition metal may be used as the free metal, or mixed or dissolved in the reacting metal. Exemplary of the compounds of these metals that may be used are titanium hydride, titanium tetra-, tri-, and dihalides such as the chlorides, bromides and iodides, the corresponding compounds of zirconium, vanadium tetra-, triand dihalides such as the chlorides and bromides, tantalum pentaand trichlorides and bromides, chromic chloride and bromide, chromous chloride and iodide, molybdenum di-, tri-, tetraand pentachlorides, etc.

Just how the transition metals or their compounds act as catalysts is not known. When the metal halides are used as the catalyst, they are generally reduced to the free metal, or to hydrides which may be nonstoichiometric compounds. It is believed that one means by which such catalysts may be effective is through their hydrides, which act as hydrogen transfer agents. However, it may be that the action is through some embrittling process which permits ready deterioration of the metal lattice structure during reaction with hydrogen. In any event, the transition metals and their compounds do effect a true catalytic action in making possible milder conditions and/or greater conversions. Since it is a catalytic action, only a catalytic amount of the transition metal or transition metal compound is needed. Generally an amount of from about 0.5% to about 10% based on the weight of metal or metals being hydrogenated is used. Higher amounts can, of course, be used, but generally do not further augment the reaction.

As has already been pointed out above, the process in ccordance with this invention can be used for the preparation of any alkali metal hydride, as for example, lithium hydride, sodium hydride, potassium hydride, etc., and for the preparation of the aluminum hydride complexes thereof, i.e. the alkali metal aluminum hydrides, such as lithium aluminum hydride (LiAll-LQ, sodium aluminum hydride (NaAlH etc.

Since some of these hydrides are more stable than others, the reaction conditions such as temperature and hydrogen pressure will be varied accordingly. The upper limiting conditions are, in general, complicated relationships between temperature and hydrogen pressure which are in turn related to the stability of the individual hydride. Thus, it is possible to operate, in a given hydride synthesis, at a higher temperature, and thus obtain higher reaction rate, provided the hydrogen pressure is sufficiently raised to prevent the reverse decomposition reaction. With less stable hydrides, for example, sodium aluminum hydride, a lower temperature and a higher pressure are advantageous, While in the synthesis of more stable by drides such as sodium hydride, higher temperatures may be tolerated. However, except where secondary solvent reactions with hydrogen may occur, generally higher pressures are more conducive of higher reaction rates, although when employing the teachings of this invention, less drastic reaction conditions will be needed for given results than when employing other procedures. For the more stable metal hydrides, the lower limit of hydrogen pressure may be as low as a few atmospheres, and the hydrogen pressure may extend upward to a thousand atmospheres with the more difiiculty synthesized hydrides. In general, the pressure will be within the range of from about 500 p.s.i. to about 10,000 p.s.i. of hydrogen pressure, and preferably will be from about 1000 p.s.i. to about 5000 p.s.i., and the temperature will be within the range of from about 80 C. to about 450 C. and more preferably from about 100 C. to about 200 C.

As already pointed out above, the process of this invention is even further enhanced when the reaction is carried out with comminution of the reaction mixture during the reaction. Such comminution may be carried out in a reactor rotating about a horizontal axis, or an axis at some angle with the horizontal. since such reactions are invariably pressure reactions, continuous connection to the gage and pressure system may be provided by a suitable inlet through the axis, and suitably provided with a packing to prevent leakage. -In such cases, the reactor is packed with generally spherical balls, such as of steel, in size or mixed sizes such as are generally em ployed-in the art of ball-milling.

A more convenient and generally preferred type of comminution reactor consists of a high pressure autoclave, with such pressuring, gaging, filling and emptying ports as may be necessary, but more specifically characterized by having a shaft and agitator so arranged as to continuously move and agitate a moving bed of balls or other attriting media. One such particularly convenient arrangement is to provide the pressure vessel, of generally cylindrical dimensions with the axis vertical, with a shaft driving an arrangement of paddles. This shaft should most conveniently be provided with a series of paddles, staggered on the shaft, both with respect to height and angular positioning on the shaft. Further, these paddles should best be of such dimensions that the outer edges reach to within a distance equal to the radius of the smallest balls used in attriting. Similarly the paddles should be pitched on the shaft in such a manner as to impart both a tangential and a vertical component to the balls. Furthermore, the bottom p'addle should be of similar specifications so as to continually sweep the bottom of the reactor relatively free of balls, and chemical species involved in the reaction. By adhering to the specification that the paddles approach the walls to within a radial distance of the smallest balls, the device will not become wedged or fouled. These dimensional limitations are particularly desirable where the internal diameter of the reactor is less than twenty times the average diameter of the balls. In height, the dimensions may be of any convenient va ue.

With reactors having diameters larger than about fifteen times the average ball diameter, due to machining difliculties and wear during use, it is frequently more desirable to provide a considerably larger clearance between the outer edge of the paddle and the reactor wall. In such cases, it has been found that a clearance in excess of 2.5 average ball diameters (*5 average radii) is conducive to proper operation.

The process of this invention is advantageously carried out in the presence of an inert, liquid, organic diluent as a solvent or slurry vehicle. Generally these diluents will be electron donor compounds which are inert under the reaction conditions, i.e. are resistant to hydrogenation, hydrogenolysis or reduction by the intermediate or final hydrides, and which at the same time provide the desirable solubility characteristics. Preferably they will be a solvent for the product, or a hydride intermediate, and not for the starting metal. Typical diluents having such characteristics are, for example, aliphatic and cyclic ethers such as diethyl ether, methyl ethyl ether, methyl propyl ether, dioxane, tetrahydrofuran, etc.; polyethers, such as diethylene glycol dirnethyl ether, triethylene glycol dimethyl ether, triethylene glycol diethyl ether, etc., aliphatic and cycloaliphatic tertiary amines such as trimethylamine, triethylamine, tri-n-butylamine, triamylamine and other trialkylamines; dialkylcyclohexylamines such as dimethylcyclohexylamine, diethylcyclohexylamine, etc., and heterocyclic tertiary amines such as pyridine, etc.

While a diluent that is a solvent or partial solvent for the product is frequently the more desirable type of diluent to use, the process of this invention is just as readily carried out using any organic liquid which is inert under the reaction conditions. Exemplary of such vehicles that may be so used are liquid saturated aliphatic hydrocarbons, as for example, hexane, n-heptane, octane, etc., or any of the commercial mixtures of saturated aliphatic hydrocarbons. Obviously, mixtures of any of these diluents can be used and in some cases may be desirable.

When employing solvents or slurry vehicles, it is generally advisable to operate with the metal or hydride reactants at as high a concentration as possible to obtain highest production from a given piece of equipment. However, there is always an upper limit of solution concentration or slurry vehicle concentration, caused by limited solubility or by a concentration above which effective milling is diflicult. These will range from a low of a few percent to an upper limit which is generally less than about 30% solids, and preferably will be within the range of from about 5 to 20% solids.

It is generally desirable to charge the metal or metal hydride reactants in a form of previous subdivision, rather thanv as massive materials. This is advantageous from the standpoint of introducing the material through the usually restricted diameter of high pressure connections, but particularly because it minimizes the comminution which must be done in the mill reactor itself. For example, sodium can be introduced as a dispersion, prepared by the means well known in the art. Other metals, such as aluminum, may be previously subdivided by atomizing in air or with an inert gas. Filings or other finely divided metals may of course be employed. It is particularly advantageous to have previously milled the metal externally, in a suitable inert vehicle, and suitably protected from oxidation, and sometimes with traces of protective getters to minimize oxidation. Previous milling renders the metal to a form of flat leaflets with a maximum of surface, and a surface which remains relatively constant during subsequent reaction until the individual particle relatively suddenly disappears. Milling, before and dur ing reaction, serves to provide a maximum constant rate during the whole reaction time.

The alkali metal hydrides and their mixed aluminum hydrides, and specifically those produced by this invention, may be used in a variety of ways known to the chemical and technological industries. In particular, bydrides, such as sodium hydride and lithium hydride, may be employed as reducing agents for organic functional groups, where it is desirable to obtain specific results, or where the use of hydrogen under pressure with catalysts is not desired. Several of the mixed metal hydrides such as lithium aluminum hydride and sodium aluminum hydride have very wide application as special purpose reducing agents, and they may also be used as solid propellant fuels when combined with suitable oxidizers, by which relatively high specific impulses are obtained.

dium aluminum hydride and lithium aluminum hydride can also be used to prepare other mixed metal hydrides, for example, magnesium aluminum hydride by reaction with anhydrous magnesium halides.

The following examples will illustrate the process of this invention. All parts and percentages are by Weight unless otherwise specified.

In each of these examples, the reaction was carried out in a mill reactor which was a 3-quart high pressure steel reaction vessel of cylindrical internal dimensions, and

about 1000 p.s.i. to about 5000 p.s.i., in an ether as dilucut, the reaction mixture being subjected to comminution by ball milling during the reaction.

2. The process of preparing sodium aluminum hydride which comprises contacting a mixture of sodium, aluminum, and at least a catalytic amount of vanadium chloride, with hydrogen at a temperature of from about 100 C. to about 200 C. and under a hydrogen pres sure of from about 1000 psi. to about 5000 p.s.i., in an ether as diluent, the reaction mixture being subjected tilted operation at Q Z i 300 It was w to comminution by ball milling durinn the reaction. vlded With means for pressurmg with hydrogen, thermo- 3 Th f r 1 h d couple for measuring the temperature of the reaction, and e P109685 0 prelfamg sqmu'm a ummilm y n a vertical agitator which had four paddles in staggered whlch coiznpnses contasung mixture of sodlum f position on the agitator shaft. Each paddle was tilted at am a "least catalync amount of a Chromlum with the vertical so as to impart a vertical as well as Chlonde, with hydrogen at a temperature of from about a tangential component to the balls. The reactor was filled to about and undfir hydrogen prfissul'e approximately two-thirds full with steel balls of inch of from about 1000 psi. to about 5000 p.s.i., in an ether diameter. For each run, the reactor was evacuated and as diluent, the reaction mixture being subjected to comfilled with nitrogen. minution b ball milling during the reaction.

Examples 18 A 4. The process of preparing lithium aluminum hy- The mill reactor in each example was charged with the Whlcnq cgmpnses contactlilga mixture of i i' given weight of metal or metals and then with the diluent, at least a cata ym amount of mamum 400 ml. each of n heptane (H) and tetrahydrofuran DYdildfi with hydrogen at a temperature of from about (THE) in Example 1; 800 ml. of n-heptane and 100 ml. 100 to about 200 n under a y e p of tetrahydrofuran in Example 2; 800 ml. of tetrahydro- Sure of fmm about 1000 P- t0 about 5 P v in an furan in Example 3; 650 m1. of tetrahydrofura or 11- ether as diluent, the reaction mixture being subjected to ethyl ether in Examples 4-7 and 700 ml. of n-heptane in comminution by ball milling during the reaction.

TABLE Alkali Grams Hydrogen Temp., Time, Percent Example Metal Grams A1 Dilucnt Catalyst Grams P13531910, 0. Hrs. Product Conv.

40 54 :50 HfIHFm TiCl3 0 4,000 150 2.57 N8AlH4--. 00 46 54 80:10H:THF Tron..- 5 4,000 150 2.25 NQAIHL. 59 45 54 THF Tim... 3 3,000 150 3.5 Nah 11in. 73 45 54 3 4, 000 150 4 NaA1H4... 00 40 54 a 4,000 150 4 NaAlH 40 54 s 4, 000 150 4 NaAlH 05 15 54 1.5 4, 500 125 5 LiAlH 65 42,5 1 5 1,000 150 2.5 NaH 100 Example 8. In Example 8 there was also charged 2 g. of 40 References Cited oleic acid as a dispersing agent for the sodium. The indi- UNITED STATES PATENTS cated amount o y l l g and i g g 550 9 5 5 1951 Finholt 23365 X the macho egj e at 9 a W 3,032,574 5/1952 Ziegler et al 260-448 hours, 2.5 hours in E amples 4o and 3 iours 1n xanr r 3,104,252 9/1963 Radd et all 260 448 ple 7. The I'GZlCllOI] DlIX -LlI'eS Wl'e h n h a t the 1 26 15 action temperature, at Whi h P Ih hy r g n p r Was 2 553 193 5 1951 Lesesne 2 4 applied. In Example 3 he re mlXiuYe was dlrecfly 3,138,433 6/ 1964- DelGuidice 23-14 heated to the reaction temperature and hydrogen pressure 2,567,972 9/1951 Schlesinger et aL 23*14 applied Without premilling. The hydrogen p es e w 2,735,820 2 0955 Steiger 23-204 X maintained by repressuring as necessary du ing th ru 0 2,884,311 4/1959 Huff 23-204 and the runs were stopped when no further pressure drop 2,920,935 1/1960 Finholt 23--14 wa obseved. The reactor contents Were then cooled, th 2,946,662 7/-1960 Mosely 23204 rans erre un er n1 ogen e 55 a after cooling the reaction mixture, the ether was removed gi: g it t by distillation and replaced by an equal volume of dry n n-heptane. The percent conversion was determined in each OTHER REFERENCES case by analysis of the product slurries. Tahulated above Cl Argewandte i VOL 73 pp. 3224,31 is the data for each of these examples. (M 1961),

Hurd, Chemistry of the Hydricles, 1952, pp. 1'81- 183.

OSCAR, R. VERTIZ, Primary Examiner.

MILTON WEISSMAN, MAURICE A. BRINDI'SI,

BENJAMIN HENKIN, Examiners. 

